EP0017348A1

EP0017348A1 - Flue gas scrubbing process using fly ash alkali

Info

Publication number: EP0017348A1
Application number: EP80300688A
Authority: EP
Inventors: Carlton A. Johnson
Original assignee: Peabody Process Systems Inc
Current assignee: Peabody Process Systems Inc
Priority date: 1979-03-06
Filing date: 1980-03-06
Publication date: 1980-10-15
Also published as: AU533856B2; CA1133236A; DE3069256D1; BR7907829A; AU5233579A; JPS6336818B2; EP0017348B1; US4228139A; NO151311C; ZA795064B; DK149603C; NO800616L; DK149603B; JPS55121825A; DK94080A; NO151311B

Abstract

The present invention relates to a fly ash utilization process or system for the removal of sulfur dioxide from the flue gas of coal fired boilers. <??>In one embodiment, a high ionic concentration is maintained in a closed loop, water balanced system which is operated at a low pH, i.e. less than 4 and preferably less than 3. The ionic concentration of the scrubber slurry is maintained at at least 5,000 parts per million of alkali metal cations, preferably over 10,000 parts per million, at least a substantial portion of which has been leached from fly ash. <??>The ionic concentration of the scrubber slurry is maintained at a high level by providing small diked areas (38, 42) in a waste pond (34) for settling of undissolved solids wherein the returned supernatant has a high ionic concentration. <??>A principal advantage of the system is that there is a substantially reduced liquid-to-gas ratio required for scrubbing SO2, with substantial savings in pumping and power requirements for the system.

Description

This invention relates to the utilization of fly ash for the removal of sulfur dioxide from flue gases.
Coal fired boilers'for power plants and the like must comply with emission standards in the United States and in other countries throughout the world with regard to both particulate fly ash and with sulfur dioxide (S0₂) emissions. In one prior art approach the problems are treated individually with the fly ash being collected for disposal and the SO₂ being removed by the lime or lime-stone slurry in a scrubber or absorber. Such a system can be represented by the flow chart shown in Figure 5 of the accompanying drawings.
In the latter system the fly ash is generally collected by use of either an electrostatic precipitator or a filter bag house.
It is also known to utilize the fly ash, however, as a source of alkali for removal of S0₂ from the flue gas, and in such case the system flow chart is as shown in Figure 6 of the accompanying drawings.
In the utilization of fly ash as a source of alkali, the fly ash is acid leached and in general the lower the pH of the leaching solution, the more alkali will be removed from the fly ash.
It is also known that to maximize the use of fly ash alkali the scrubber system should be operated at a pH of 4 or less.
The sulfur content as well as the ash and alkali content of coal varies from place to place over a considerable range. The use of fly ash as an alkali source depends upon the ratio of calcium and other cations to the amount of sulfur in the coal.
In a lime or limestone S0₂ flue gas scrubbing system the slurry is recirculated through an absorption tower for contact with the flue gas to be cleaned. The S0₂ is thus dissolved in the water phase of the scrubbing medium to produce sulfurous acid. In such a lime or limestone system calcium ions are produced by dissolution of calcium hydroxide or calcium carbonate which then reacts with the absorbed S0₂ to produce an insoluble solid precipitate. In the utilization of collected fly ash, however, the cations to react with the S0₂ can be provided all or in part by the acid leached fly ash rather than by the addition of lime or limestcne to the scrubbing slurry.
It is an object of the present invention to provide an improved flue gas scrubbing process using fly ash alkali.
According to the present invention, there is provided a process of utilizing fly ash for the removal of sulfur dioxide from flue gas, comprising:

A. acid leaching fly ash to provide a high ionic strength scrubber slurry;
B. contacting the flue gas with said scrubber slurry at a pH of about 4 or less; and
C. maintaining the ionic concentration of the scrubber slurry at a high concentration by recycling the scrubber slurry supernatant in a closed loop, water balanced system.

The process embodying the invention utilizes fly ash for the removal of sulfur dioxide from flue gas by acid leaching the fly ash to provide a high ionic strength scrubber slurry and maintaining the high ionic concentration in a closed loop water balanced system and contacting the flue gas with the scrubber slurry at a pH of less than about 4, preferably less than a pH of 3. The ionic concentration of the scrubber slurry preferably is maintained at over about 5,000 parts per million of alkali metal cations and more preferably over 10,000 parts per million of alkali metal cations in the scrubber slurry. The closed loop water balanced system utilizes a small volume waste reservoir with a return of scrubber slurry supernatant from the waste reservoir so that the ionic concentration of the supernatant is not permitted to be diluted prior to removal of the supernatant. The preferred method of maintaining the ionic concentration of the scrubber slurry is to provide small diked areas in a waste pond where scrubber slurry and undissolved solids are initially received and after some settling of solids the supernatant is returned to the scrubber from the relatively small volume diked area of the pond. As the first small diked area in the waste pond is filled with solids, successive diked areas are created to maintain the ionic concentration of the scrubber slurry supernatant as the scrubber slurry and undissolved solids are again directed to each successive small receiving reservoir for the scrubber waste. A thickener and filter system may also be used to recover high ionic concentration slurry supernatant in the system. The system is water balanced, e.g. only enough make up water is added to the system to replace that lost by evaporation or entrainment in removed solids. The maintaining of a high ionic concentration in the scrubber slurry substantially reduces the liquid to gas ratios involved with substantial savings in pumping and power reauirements for operating the system. Iri another embodiment of the invention a wet venturi scrubber is preferred for collecting the fly ash. The use of the wet venturi scrubber eliminates problems associated with fly ash handling and integrates the fly ash removal into the S0₂ scrubber loop.
In order that the invention may be more readily understood, reference will now be made to the accompanying drawings, in which:-

FIGURE 1 is a flow sheet and schematic drawing of a process embodying the invention, showing a multiple diked area waste pond for return of supernatant to the scrubber loop;
FIGURE 1A is an alternate embodiment of the invention showing the use of a thickner and filter system for return of supernatant to the scrubber loop;
FIGURE 2 is a typical graph showing the per cent of unreacted alkali as a function of pH in typical acid leaching of alkali from fly ash;
FIGURE 3 is a typical graph showing performance curves illustrating the efficiency of SO₂ removal as a function of liquid to gas ratic (L/G) for a typical limestone wet scrubbing system and a wet scrubbing fly ash alkali system embodying the invention, each at an optimal constant pH;
FIGURE 4 is a graph showing the typical increase in SO₂ removal as the total dissolved solids in the scrubber slurry increases; and
FIGURES 5 and 6 are flow charts of the previously discussed prior systems.

Referring to Figures 1 and 1A, the scrubber system embodying the present invention is schematically shovm, and there is provided an S0₂ absorber 10 having a number of snray heads or nozzles 12 for contacting scrubber slurry with flue gas which is first passed through a fly ash collector 14 which is preferably a wet venturi. The fly ash is then acid leached in the scrubber system to provide alkali cations to the scrubber slurry. The flue gas exits from the fly ash collector via duct 14a to flow upwardly through the absorber 10 and out of conduit 16 as cleaned flue gas.
The SO₂ from the flue gas is absorbed in the sprayed scrubber slurry and is collected in the slurry recycle tank 18. Pump 20 pumps the scrubber slurry through conduit 22 back to the spray heads 12 with any makeup water required being introduced by a conduit 24 and spray head 26.
Pump 28 and conduit 30 provide scrubber slurry to spray head 32 in the wet venturi for the collection of fly ash. The advantage of using a wet venturi is that there is no further handling of fly ash required in the system since the collected fly ash is flushed into the slurry recycle tank.
It is also understood that one or more trays or other contacting devices may be used instead of spray heads or nozzles 12 in the absorber 10.
Referring to Figure 1, scrubber slurry and undissolved solids including fly ash barticulate and alkali metal sulfates and sulfites are conveyed to a waste nond 34 via conduit 36. However, instead of merely dumping the slurry and undissolved solids into the waste nond and permitting the slurry supernatant to become dilute, the slurry is fed into a first diked area 38 which constitutes only a small portion of the pond to permit settling of the undissolved solids while the supernatant from area 38 is returned to the slurry recycle tank via conduit 40.
By diking off a relatively small area of the waste pond, a high ionic concentration of alkali cations is returned to the slurry recycle tank in the supernatant from the small segregated area of the waste pond. As the first diked area 38 fills up with undissolved solids, a second diked area 42 of the pond is then used t. receive the scrubber slurry with undissolved solids and the supernatant return conduit 40 is positioned to remove supernatant from area 42. The second diked area may be put into use before the first diked area is completely full of undissolved solids by use of an overflow pipe or channel 44 between the two areas. In such case the inlet conduit 36 would still empty into the first diked area while the supernatant return conduit 40 would be positioned in the second diked area.
By the use of such a system, the ionic strength of the returned supernatant is maintained at the highest ionic strength possible, i.e. in excess of 5,000 ppm and preferably in excess of 10,000 ppm. The maintenance of the high ionic concentration in the supernatant substantially reduces the liquid to gas. ratio and conse- ^quently reduces the amount of pumping horsepnwer required to circulate the scrubber slurry.
Referring now to Figure 1A, in an alternate embodiment of the invention, it will be seen that a thickener 46 may be used to receive slurry and undissolved solids through conduit 48 with supernatant being drawn off by conduit 50 to supernatant tank 52 for return to the scrubber.loop via pump 54 and conduit 56. Pump 58 and conduit 60 pass the concentrated solid slurry from the thickener to a vacuum filter or centrifuge where filter cake is removed as at 62 with the supernatant being returned to the supernatant tank via conduit 64. Thus the return of the supernatant in the system shown in Figure 1A will also have high ionic concentration as in the system shown in Figure 1.
Fly ash is a complex material and varies in its chemical components depending upon the source of the coal which is burned. Typical fly ash analyses are as follows:
As seen in Table 1 above, fly ash, although differing somewhat in its chemical makeup, generally has sufficient alkali cations for an S0₂ scrubbing system. The fly ash can be preliminary tested to determine if it has sufficient alkali cations for use in such scrubbing system by extraction of fly ash samples and titration to determine the theoretical alkali available in the fly ash used. The procedure is generally to slurry a fly as sample in water and titrate with sulfurous acid. The pH resulting from the addition of specific quantities of the acid is then measured. The amount of acid used for a given pH is directly related to the amount of alkali extracted from the fly ash sample. The percentage of the theoretical alkali of fly ash unextracted as a function of pH can then be plotted. The typical shape of the curve obtained from such laboratory test data is shown in Figure 2.
Various fly ash samples have been tested and most show similar characteristics. At high pH, e.g. 9 or higher, few alkali cations are extracted. But as the pH drops more alkali cations are extracted until a plateau is reached in which the amount of alkali is almost constant. As the pH continues'to drop there is a very sharn increase in the availability of alkali cations in the fly ash. This generally occurs at pH values of approximately 4 or less. Thus to obtain the greatest benefit of alkali cations extracted from the fly ash, the scrubbing recycle slurry should be operated at a pH of 4 or less, preferably 3 or less. The combination of low pH and high ionic concentration of alkali metal cations provides substantial savings in the scrubbing of flue gas from coal fired plants with fly ash extraction.
In practicing the process embodying the present invention in a pilot plant system at a pH of around 2.5 with ionic concentration of the alkali cations being from about 10,000 to 45,000 ppm, SO₂ emission standards were achieved using only the alkali from fly ash with no suplemental alkali being required, thus eliminating significant operating costs.
In a conventional lime or limestone scrubber system the liquid to gas (L/G) ratio reflects the litres of scrubber slurry required approximately per 623 cubic metres per minute of the flue gas (gallons per 100,000 cfm) and is a direct measure of the pumping horsepower required for the system. It is known that the L/G ratio increases significantly as the pH of the slurry decreases and it would appear that under pH conditions required for optimal alkali extraction from the fly ash, i.e. a pH of 4 or less, that there would be a penalty in the required pumping horsepower for efficient SO₂ removal. It has been found however that when the ionic concentration of the alkali cation in the scrubber liquid is maintained at a high level, that the same SO₂ removal efficiency can be obtained at its significantly lower liquid to gas ratio, with consequent power savings in required pumping horsepower. A typical performance curve showing SO₂ removal efficiency as a function of liquid to gas ratio for both a limestone system and a fly ash alkali system are shown in Figure 3. As seen in Figure 3, the fly ash alkali system has a steeper curve at about the 50 per cent SO₂ removal point, indicating that it is more efficient as to pumping horsepower than a limestone system for removal of SO₂ from flue gas.
At low SO₂ removal efficiencies, (e.g. 20-30 per cent) there is not much difference in L/G requirements between the systems, with the limestone system requiring somewhat less than that required for fly ash alkali systems. Most SO₂ removal systems have high efficiency requirements, however, and the reduced L/G ratios for the fly ash system can result in savings of 20 per cent or more of the pumping horsepower required for SO₂ removal.
In the fly ash there are a number of cations besides calcium which are extracted in varying degrees. Accordingly, the chemistry of the system becomes analogous to an internal dual alkali system. A typical analysis of the liquid phase of the recycle slurry is shown below in Table II.
Operating data from the pilot plant have verified the importance of maintaining high ionic strength in the scrubbing system to achieve higher SO₂ removal efficiency. In these tests the scrubber was operated under varying ionic concentrations as expressed by total dissolved solids with all other factors remaining unchanged. The results are shown in the graph of Figure 4 wherein the L/G ratio was held constant. As shown in Figure 4, the per cent of SO₂ removal continues to rise even after 10,000 or 20,000 ppm total dissolved solids are present in the scrubber slurry. It has been found that there should be at least 5,000 ppm of total dissolved solids and preferably over 10,000 ppm up to the economically practical or solubility limit of the slurry.
The system embodying the invention should be operated at the highest ionic strength possible for greatest scrubbing efficiency at the lowest L/G ratio. This is achieved by operating the system under a totally closed loop water balance with only enough makeup weter added to the system sufficient to meet the evaporative load and the entrained water in the waste solids. This minimizes the amount of waste water effluent from the system and results in further economies in the small amount of waste water needing treatment.
In conventional lime or limestone scrubbing systems the waste solids are mainly calcium sulfite with some calcium-sulfate. The ratio of the components vary with the operating conditions of the system, but in general the greater parts of the waste solids is calcium sulfite which is thixotropic and difficult to dewater in a waste solid disposal system. Under the fly ash utilization system substantially all of the waste solids are naturally oxidized to calcium sulfate which is very insoluble and relatively easy to dewater. The use of a fly ash alkali scrubbing system shows significantly greater bulk settling rates and the undissolved solids can be concentrated in a thickner to well over 50 per cent solids with thickner underflow producing a filter cake or about 85 per cent solids, which is easily handled and his a dry sand-like granular appearance.
In conventional limestone 002 removal systems there are also scaling problems created by the precipitation of super-saturated calcium sulfate which deposits on the absorber surfaces. Control of the super saturation ratio limit (actual solubility to the theoretical solubility of calcium sulfate) is necessary to prevent scaling. Fly ash alkali utilization systems can be operated with super saturation ratios of 1.0 and accordingly, there is little or no calcium suJ- fate scaling.
The system embodying the present invention thus provides substantial economic benefits by: (1) reducing or eliminating the cost of alkali, (2) substantial reduction in power consumption (pumping horsepower), (3) reduction in initial capital investment, (4) reduction in waste solids handling and disposal costs, (5) improved system reliability with minimal risk of scaling.

Claims

1. The process of utilizing fly ash for the removal of sulfur dioxide from flue gas, comprising:

A. acid leaching fly ash to provide a high ionic strength scrubber slurry;

B. contacting the flue gas with said scrubber slurry at a pH of about 4 or less; and

C. maintaining the ionic concentration of the scrubber slurry at a high concentration by recycling the scrubber slurry supernatant in a closed loop, water balanced system.

2. The process claimed in claim 1, which comprises recycling the scrubber slurry supernatant in a closed loop water balanced system having a waste reservoir (34) into which scrubber slurry and solids flow after said scrubber slurry has contacted the flue gas and from which the scrubber slurry supernatant flows to recontact the flue gas, said waste reservoir having a relatively small volume thereby to retain high ionic concentration of the scrubber slurry supernatant which is returned to recontact the flue gas.

3. The process claimed in claim 2, which includes introducing the scrubber slurry and solids into a relatively small inlet area (38) of a waste pond which comprises said waste reservoir (34), and returning the scrubber slurry supernatant from said inlet area, said inlet area being at least partially segregated from the remainder of the pond by a dike.

4. The process claimed in claim 3, wherein the diked inlet area is the first of a succession of small diked areas (38, 42) provided in the waste pond, the or each successive diked area receiving scrubber slurry and undissolved solids as the or each prior diked area is substantially filled with waste solids.

5. The process claimed in any preceding claim, which comprises maintaining the ionic concentration of the serubber slurry at about 5,000 ppm or more.

6. The process claimed in claim 5, which comprises maintaining the ionic concentration of the scrubber slurry at about 10, 000 ppm or more.

7. The process claimed in any preceding claim, which includes collecting the fly ash from the flue gas by means of a wet venturi scrubber (10) .

8. The process claimed in any preceding claim, which includes acid leaching the fly ash to provide a scrubber slurry having at least several different alkali metal cations extracted from fly ash, and contacting the flue gas with the scrubber slurry while maintaining a high ionic concentration of said alkali metal cations in the scrubber slurry.